Resin composition



Patented Apr. 26, 1949 Frank J. Soday, Baton Rouge,

La., assignor to The United Gas Improvement Company, a corporation of Pennsylvania No Drawing. Application June 20, 1944,

Serial No. 541,259

1 Claim. 1 3

This invention pertains to the use of certain hydrocarbon resins in coating compositions.

More particularly, this invention relates to the use in coating compositions of resins derived by the polymerization, by thermal and/or catalytic methods of the high boiling hydrocarbon material separated in monomeric form from tar formed during the production of combustible gasv by processes involving the pyrolytic decomposition of petroleum oil with or without the aid of catalysts in conjunction with phenolic and more particularly substituted phenolic resins.

A feature of the invention is the provision of drying oil coating compositions comprising a mixture of resins of the type described dissolved in a bodied drying oil. Pigments, fillers, coloring agents, driers, anti-skinning agents, plasticizers, solvents, particularly hydrocarbon solvents, and/ or other additives, also may be incorporated in such coating compositions, if desired.

This invention is based upon the discovery that a blended resin possessing unexpectedly outstanding coating properties may be obtained by incorporating a hydrocarbon resin of the type to be more particularly described herein with one or more phenolic, and more particularly substituted phenolic resins.

Such blended resins are soluble in, or compatible with, the less expensive drying oils, such as, for example, linseed, fish, perilla, soya, and similar oils, or mixtures thereof, and the less expensive solvents, such as hydrocarbon solvents, for example, mineral spirits and V. M. 8; P. naphtha and/or mixtures thereof with aromatic hydrocarbons. Thus, they are ideally suited for the preparation of inexpensive compositions designed to coat a wide variety of surfaces, such as wood, metal, cement, concrete, brick, ceramic, or other surface.

Such resinous blends also may be used with the more expensive drying oils, such as tung oil, oiticica oil, dehydrated castor oil, conjugated linseed oil, and the like, with excellent results.

Coating compositions prepared from such blends possess outstanding coating characteristics. When applied to a given surface the resulting film is unusually mar resisting, alkali resisting, water resisting, and wear resisting. In addition, it is quite glossy in appearance and possesses excellent exposure characteristics, evenwhen exposed to bright sunshine and salt air conditions.

The hydrocarbon constituents of petroleum tar of the type described have usually been considered to comprise residual tar, dead oil, and light oil. The residual tar comprises the heavy black pitch constituents of the tar, together with any oil unseparated therefrom. The dead oil comprises oil separated from the residual tar and boiling higher than, say, 200210 C. The light oil comprises oil separated from residual tar and boiling lower than, say, ZOO-210 C. v a

It has been discovered that very considerable quantities of such resin-forming unsaturated monomeric material above referred to, including large quantities of readily heat polymeriza-ble material, may be contained in the tar produced in the vapor phase pyrolysis of crude petroleum oil or a fraction or fractions thereof, such as, for example, gas oil or residuum oil. This is particularly so in the case of petroleum oil gas tar produced when the pyrolysis is conducted at relatively high temperatures, such, for example, as in the manufacture of oil gas or carburetted water gas at average set temperatures above 1300 F. and also particularly so when the oil pyrolyzed is naphthenic, such as a crude oil classifiable in classes 5 to 7, inclusive, according to the method of classification described in Bureau of Mines Bulletin 291, as modified by Bureau of Mines Report of Investigations 3279, or a fraction or fractions of such an oil.

The possibility of recovering large quantities of resin forming monomeric unsaturated material boiling in the dead oil range was long unrealized. This was because the usual distillation procedures for the purpose of petroleum tar dehydration and/or tar fractionation were such as ,to polymerize the readily heat polymerizable monomers boiling in the dead oil range into heavy polymers, which were inextricably mixed with the heavy I black residual pitch constituents and lost therein.

In copending application Serial Number 370,608, filed December 18, 1940, by Edwin L. Hall and Howard R. Batchelder, which has matured into Patent 2,387,259, granted October 23, 1945, such heat polymerizable monomeric hydrocarbons boiling in the range of from 210 to 450 C. and

separated from the heavy black pitch constituents of the petroleum tar are described and claimed, together with heat polymers produced therefrom.

In copending application Serial Number 386,232, filed April 1, 1941, by Waldo C. Ault, which has matured into Patent 2,387,237, granted October 23, 1945, there is described and claimed the production of catalytic resins from the heat polymerizable and/or catalytically polymerizable monomerichydrocarbons boiling within the range of from 210 C. to 450 C. and separated in monomeric form from the heavy black pitch constituents of the petroleum tar.

In the manufacture of oil gas and carburetted water gas, the tar produced is usually in the form of an-emulsion due to the condensation of hydrocarbon constituents from the gas in the presence of water simultaneously condensed from the gas or otherwise present.

In copending application 342,735, filed June 27, 1940, by Edwin L. Hall and Howard R. Batchelder, which has matured into Patent 2,366,899, granted January 9, 1945, there is described a method of dehydrating such petroleum tar emulsions and of fractionating the hydrocarbon constituents thereof by rapid distillation with the separation from the heavy pitch constituents of residual tar of such heat polymerizable unsaturated monomeric hydrocarbons boiling in the dead 011 range.

In copending application 353,034, filed August 17, 1940, by Howard R. Batchelder, which has matured into Patent 2,383,362, granted August 21, 1945, there is described the dehydration of such petroleum tar emulsions and the fractionation of the hydrocarbon constituents thereof with the recovery of monomeric unsaturated heat polymerizable dead oil constituents separate from the heavy black pitch constituents of residual tar, by the solvent extraction of the emulsion with a hydrocarbon solvent such as liquefied propane or butane.

Other processes, for example fractional condensation, might be employed to recover these relatively high boiling unsaturated hydrocarbons in monomeric form and separate from the heavy black pitch esses for oil pyrolysis which avoid the formation of emulsions, may be employed for the production of the monomeric material. Furthermore, while it may be preferred to employ for pyrolyconstituents of the tar.- Also, procsis petroleum oils or cuts therefrom, which are I classifiable in classes 5 to 7 inclusive according to Bureau of Mines Bulletin 291, modified as above indicated,- and particularly those in class 7, other oils may be employed. v

Whatever process of oil pyrolysis is employed in the production of this monomeric material, and whatever process is employed for separating the resultant tar, a very important factor is the exercise of care in the treatment of the tar in order to avoid excessive polymerization of these readily heat polymerizable dead oil constituents and their loss as polymers mixed with the heavy black pitch constituents of the residual tar.

As a result of separation of the light oil and dead oil components of the products of such petroleum oil pyrolysis from the residual tar, without polymerization or with materially reduced polymerization, a substantially pitch-free hydrocarbon material may be separated havin a portion boiling within the range of from 210 to 450 C., and particularly between 210 C. and 350 0., which may contain from 5% to 30%, and higher, of monomeric unsaturated hydrocarbons readily polymerizable by heat.

The particular concentration of this heat polymerizable monomeric material obtained in a. given case willv depend upon the amount of polymerization produced in separating it from the residual .tar, as well as upon such factors as the conditions of pyrolysis and the character of the petroleum oil pyrolyzed.

As previously stated, the above mentioned heat polymerizable monomeric material may be readlly polymerized by heat to form valuable resins.

Polymerization may be efiected by heating the total material separated from the residual tar sufliciently to p lymerize the readily heat poly- 4 merizable monomers boiling within the range of from 210 to 450 C., but insufllciently to appre-- ciably polymerize the heat polymerizable material contained in lower boiling ranges, such, for instance, as methyl styrenes and styrene. Thismay be accomplished, for example, by heating with stirring for 4 hours at 200 0., followed by distillation under vacuum to isolate the resin.

It may be preferable, however, .to first effect a separation by fractional distillation between light oil boiling below, say, 210 C. and dead oil boiling above, say, 210 C.

The heat polymerizable monomeric material boiling within the range of'210 to 450 C. is so readily polymerizable by heat, that, in the fractional distillation of the light oil from the dead oil, a portion of the monomeric material is usually unavoidably polymerized and remains as polymer dissolved in the other constituents of the dead oil after the light oil is taken off overhead.

ed dead oil may be effected by heating the dead oil with stirring, for example, for four hours at The resin thus produced, together with any resin produced during the separation of the light oil from the dead oil, may then be isolated by distillation under vacuum.

In the separation of lower boiling hydrocarbon material from the pitch c-ontituents of residual tar by various methods, the oil separated may contain components boiling above 350 C. and there may be present heat polymerizable monomeric material boiling outside the range of from 210 C. and 450 C. together with the monomeric material boiling within that range. On polymerization therefore the resin may include polymers derived from monomers boiling outside saidyrange along with polymers derived from monomers boiling within said range.

As herein before stated; after polymerization the resin may be isolated by distillation in vacuum, which may be assisted by steam. The yield, melting point, and other characteristics of the resin will depend upon the extent to which the isolation has been carried, or, in other words, upon the proportion of associated oils left in the resin.

Exhaustive steam distillations of the resins obtained from the unsaturated monomeric mate- ,rial isolated from tar by the distillation or solparatus described in A. S. T. M. Procedure D6l-24,

with the following modifications:

1. Mercury is employed in depth of 12 /2 inches instead of water.

2. The cube of resin is rigidly supported by clamping the hook upon which the resin is attached so that the top of the cube is 1 inch below the surface of the mercury.

3. A /2 inch immersion thermometer is employed and is immersed to that depth.

4. The exact temperature at which the resin becomes visible at the surface of the mercury is recorded as the softening point of the resin.

5. The melting point of the resin is calculated from the softening point by the following formula:

Melting point C.=

Softening point C. l.25+2 C.

The melting point of the resins described in this specification is intended to mean melting point, as determined by the above recited method, unless otherwise specified.

Lower melting point resins may be readily obtained in greater yields by less exhaustive removal of the associated oils, thus resins ranging from very soft to hard resins having high melting points may be obtained as desired.

It has been usually found that each 6% of associated oils left in the resin lowers the melting point about 10 C.

Heat resins having melting points of 120 C. have been readily produced in yields corresponding to 20 to 30% of the dead oil in the case of the tar distillate produced in accordance with the process described in copending application Serial No. 342,735, and resins of the same melting point have been obtained in yields as high as 60% of the dead oil in the case of dead oil separated from extract produced in the process described in application Serial No. 353,034,

The heat polymerizable unsaturated monomeric material is preferably in suflicient concentration in thatportion of the hydrocarbon material separated from the residual tar which boils within the range of from 210 to 450 C. to produce on polymerization by heat a, 120 C. meltingpoint resin in quantity equal to at least 10 percent of the hydrocarbon material boiling within the range from 210 C. to 450 C., and preferably at least 20 percent, or higher, but lower concentra tions may be employed.

The color of the resins obtained may-vary from yellow to dark brown.

Heat polymer resins produced from dead oil separated'from residual tar by the distillation process described in said copending application, Serial No. 342,735, have shown a tendency to be lighter in color than those produced from dead oil obtained from the solvent extraction of tar with propane and butane as described in said copending application, Serial No. 353,034. Also, heat polymer resins produced from the lower boiling portions of. the dead oil have shown a tendency to be lighter in color than heat polymer resins produced from the higher boiling portions, especially such a portion as that boiling in a dead oil cut taken from 180 C. to 210 C. under a vacuum equivalent to 20 mm. of mercury, absolute. The following examples will serve to illustrate the preparation of resins from such unsaturated fractions by thermal polymerization methods.

. Example 1 Approximately 1000 grams of dead oil derived from the rapid distillation of oil gas tar in accordance with the process described in said copending application,- Serial No. 342,735, and subsequent separation of the distillate, was weighed into a 2-liter 3-necked' flask equipped with a thermometer and a short reflux condenser. The oil was then slowly stirred and heated over a Bunsen burner at a liquid temperature of 200 C. (:10" C.) for a period of 4 hours. 1

At the conclusion of this period, the material was allowed to cool somewhat and was then transferred for distillation to a tared 2-liter flask equipped with a ground glass neck,

The oil wasaccurately weighed at this point.

The flask was provided with means for measuring vapor temperatures and was connected with condensing apparatus and with means for providing a vacuum including a pressure control device. Bumping during distillation was avoided by folding several folds of iron wire to such length that one end reached slightly into the neck of the flask while the other end rested on the bottom of the flask.

The pressure was reduced to 100 mm. Hg, absolute and heat applied by means of a Bunsen burner. The distillation was continued at a pressure of 100 mm. Hg absolute, until the vapor temperature'reached 180 C. During this first stage of the distillation, care should be exercised to prevent crystallization of naphthalene, if present, such as by employing a condenser operating at elevated temperatures.

When the vapor temperature reached 180 C. at a pressure of 100 mm. Hg, absolute, the flame was lowered and the pressure gradually reduced to 20 mm. Hg, absolute, using care to avoid bumping. When a pressure equivalent to 20 mm. Hg, absolute, was reached, the pressure was maintained at that value, and the distillation continued until a vapor temperature of 195 C. was reached.

During the second stage, the condenser may be cooled by cold water, but care should be taken to avoid the solidification of anthracene, if present.

The distillation was conducted rapidly, 5 to 10 cc. of oil per minute being removed.

When a vapor temperature of 195 C. was reached, the source of heat was removed and air was permitted to enter the apparatus slowly until atmospheric balance-was restored.

In the above operation the yield of resin was 29.3%, with an actual melting point of 128 C., which was calculated to be equivalent to a yield of 31.4 at a melting point of 120 C. The color of the resin was light brown.

A straight run A. S. T. M. distillation of 100 cc.

- of the original oil gave the following data:

As pointed out previously, the high boiling monomeric material derived from tar obtained in the pyrolysis of petroleum, by rapid distillation or solvent-extraction methods, may be polymerized to form resins of the type desired by the application of certain catalysts, either with or without the simultaneous, or otherwise, application of heat.

Catalysts such as mineral acids, for example, sulfuric acid, hydrogen chloride, acids of phosphorus, or acid acting metallic halides or complexes of said halides, preferably organic solvent complexes, as for example, boron trifluoride, aluminum chloride, boron trifluoride-diethyl ether complex, boron trifluoride-dimethyl ether complex, boron trifluoride-phenyl ether complex, boron trifluoride-phenyl methyl ether complex, boron trifluoride-dioxan complex, boron tri fluoride-toluene complex, corresponding a1u-' minum chloride complexes, and the like, may be employed for this purpose.

The metallic halides and their complexes employed are characterized by their ability to hydrolyze in the presence of water to give an acid As an example of a convenient procedure for the production of resins of the type desired with the use of sulfuric acid as catalyst, the following is given.

Emample 2 A sample of the oil to be polymerized, say 500 cc., is poured into a two-liter 3-neck flask equipped with a thermometer and stirrer, To the oil is added 96% H2804 while agitating vigorously. The acid is added 1 cc. at a'time and the temperature is not permitted to exceed 50 C. The addi' tion of the acid is continued in this manner until no further temperature rise is noted. The amount of acid necessary to achieve this end has been found-to be about 1%, by volume, of the oil present. 1

The oil then is diluted with approximately an equal volume of naphtha, toluene, or similar diluent, and the solution decanted into 500 cc.

of warm water (approximately 60 C.), leaving I the acid sludge behind.

After settling, the water layer isdrawn off, and neutralization of the acid is accomplished by use of a 10% to 20% aqueous solution of sodium hydroxide. After Washing with caustic, an additional water wash may be made, In either case, the resin solution is dried by filtration through a bed of a suitable drying agent, such as lime.

If desired, the diluent may be added before polymerization instead of after polymerization.

After neutralization and drying, the resin may be isolated from the unpolymerized oil by any desired method, or the resin may be concentrated therein by vacuum distillation, which may be assisted by steam. The melting point of the resin and the yield obtained will depend, among other things, upon the extent to which the resin has been removed from the unpolymerized oil.

A convenient procedure for the production of resins of the type desired by the polymerization of monomeric unsaturated material, derived from tar resulting from the pyrolysis of petroleum, with the use of metallic halide catalysts or metallic halide-organic solvent complex catalysts is illustrated in the following examples.

Example 3 A 10 gram portion of the selected catalyst is suspended in 300 cc. of benzene by stirring. A 300 cc. portion of the dead oil separated from distillate recovered from petroleum tar emulsion by flash distillation as described in said copending application, Serial No. 342,735, is added dropwise from a separatory funnel while maintaining the temperature of the reaction mass below 50 C. When the addition has been completed, the mass is stirred for a period of 2 hours and then neutralized with an aqueous solution of sodium hydroxide (10 to 20%). Stirring is continued for an additional hour.

Clay or any other desired filter aid then is added and the mass is filtered. The aqueous layer is separated and discarded, after which the treated material is washed with hot water until the washings are neutral to litmus. The treated material then is filtered through lime to remove water or otherwise dried, and the resin isolated by any desired method.

Example 4 A 532.6 gram portion of this unsaturateddead oil was treated with 8 cc. of 66 B. H2804 according to the procedure described in Example 2. Toluene was added after polymerization. Approximately 42% of the dead oil was converted to resin having a melting point of 97 C. and a brown color. The end temperature of the distillation for the removal of oil from the resin was 192 C. and the end pressure was equivalent to 18 mm. of mercury, absolute. A-total of 145.9 grams of oil was recovered. The calculated yield of resin having a melting point of C. was 36.2%.

As pointed out previously, the unsaturated dead oil employed for the preparation of resins of the type desired may be polymerized by (a) thermal means, (1)) catalytic means, or (0) 9.00mbination of thermal and catalytic means. In the latter case, the processes may be carried out consecutively without the intermediate removal of resin, or the resin may be removed between successive treatments.

The unsaturated dead oil used in the following example was obtained from petroleum tar emulsion by the process of copending application Serial Number 342,735. After separation from light oil, it was treated to remove heat polymerizable unsaturates by heating at 200 C. for 4 hours, followed by removal of the heat polymer resin formed. It was then subjected to catalytic polymerization by the following method.

ExampZeS A 500 gram portion of the said unsaturated dead oil was treated with 6 cc. of 66 B. H2S04 according to the method described in Example 2. Naphtha was added after polymerization. Approximately 19% of the dead oil was converted to resin having a melting point of 882 C. and a light yellow brown color. The end temperature of the distillation for the removal of oil from the resin was C., and the end pressure was equivalent to 20 mm. of mercury, absolute. A total of 407.9 grams of oil was recovered. The calculated yield of resin having a melting point of 120 C. was approximately 15% Examination of the monomeric unsaturated material and associated oil boiling within the range of from 210 to 450 C. described herein and the resins produced therefrom have shown that these materials are predominately aromatic.

Density determinations have indicated that the density of 25 C. of the resins obtained-as above described frequently falls within the approximate range of 1.12 to 1.20, with resins produced from dead oil from the solvent extraction of tar tending to be somewhat higher than those produced from dead oil from rapid tar distillation. Thedensities of the acid polymers tend to be somewhat lower than those of the heat polymers derived from the same unsaturated dead oil. Resins of this type having other densities may be employed, however.

The molecular weights of the resins produced as previously described necessarily vary with the melting point, which also varies with the presence cube in mercury method.

The fracture of the high melting point resins describedherein may range from conchoidal to hackly. In general, the polymers are quite brittle.

l The resins described herein, except those hardened by exhaustive steam distillation to a very high melting point, will usually react positively to the anthraquinone reaction, indicating the presence of anthracene, unless produced from lower boiling portions of the dead oil, which do not contain anthracene, or unless the anthracene has been otherwise removed.

The resin described herein usually will give but a slight diazo reaction, indicating the substantial absence of phenols.

The resins produced as above described usually will give negative Lieberman Storch reactions, indicating the absence of rosin acids.

Upon thermal decomposition of the resins of the type produced as above described herein, appreciable yields of material boiling within the range from 210 C. to 450 C. will be produced.

The heat polymer resins of the type producedas above described usually are substantially completely soluble in carbon disulfide and benzol. The quantity of resin insoluble in a mixture containing 50% petroleum ether and 50% pentane varies with the melting point of the resin, and may be of. the order of 52% in the case of a thermal resinhaving a melting point of 95 C. and of the order of 80% in the case of a thermal resin having a melting point of approximately 183 C. (Cube in mercury method.)

The quantity of resin of the type-produced as above described insoluble in a mixture of 50% petroleum ether and 50% pentane, but soluble in C014, may be of the order of 50% for a thermal resin having a melting point of 95 C. and of the order of 74% in the case of a thermal resin having a melting point of 183 C. (Cube in mercury method.)

The quantity of thermal resin insoluble in both the petroleum ether-pentane solution and C014 usually is very low, ranging from afraction of a percent to the neighborhood of 6 or 7% In general, catalytic polymers are much more soluble than heat polymers from the same unsaturated dead oil in all solvents except the alcohols.

The polymers from unsaturated dead oils obtained from the rapid distillation process described in copendlng application, Serial No. 342,- .735, tend to be more soluble in those solvents tried than similarly produced polymers from unsaturated dead oils obtained by the solvent extraction process described in copending application, Serial No. 353,034.

The above described characteristics'of color,

density, fracture, melting point, molecular weight, diazo reaction, Lieberman Storch reaction, anthraquinone reaction,.thermal decomposition, and solubility are given for the purpose of illustration. It is not intended to imply necessarily that the resin produced as described above and employed herein may not depart somewhat from this illustrative description in one particularor more. I

Furthermore, the addition of other materials to the heat polymerizable monomeric unsatiirated I materials prior-to polymerization or to the resins after polymerization may of course modify the properties of the resins produced. Examples of such materials are other synthetic or natural resins, plasticizers,- softeners, fillers, coloring materials, etc.

In separating such material, the dead oil con- The resin employed may comprise mixed polymers of monomeric material boiling within the range of from 210 C. to 450 C., together, if desired, with polymers of monomers boiling outside of this range, or resins may be employed which are produced from monomers boiling within a selected range or ranges within the range of from 210 C. to 450 terial boiling above, say, 250 C. or, say, above taining the monomers may be fractionated*by distillation under vacuum, assisted by steam, to avoid undue polymerization during the separation, or other methods of separation-may be employed. 4

As previously pointed 'out, the blend of hydrocarbon resin of the type described and one or more phenolic, particularly substituted phenolic, resins possesses unusually good properties which 1 render it of outstanding value for use in coating compositions. Among these outstanding proper ties are its unusually good alkali and water resistance, its excellent drying characteristics, and its pronounced hardness, imparting long wearing characteristics to coating compositions prepared therefrom.

Examples of phenolic type resins of the type more particularly desired for the preparation of resin blends of the type described herein are the substituted phenolic resins derived by reacting one or more substituted phenols, particularly aikyl and/or aryl substituted phenols, cresols,

xylols, catechols, and the like, with one or more aldehydes, particularly formaldehyde. Examples of substituted phenols, are the mono-, di-, or trihydroxylated benzenes containing one or more alkyl substituents, such as methyl, ethyl, propyl, butyl, amyl, or the like, and/or aryl substituents such as phenyl, tolyl, and the like. M

I prefer to use phenolic type resins derived by the reaction of an aldehyde and particularly formaldehyde with one or more monoalkyl and/or monoaryl substituted monohydroxylated benzenes, for example, isobutyl phenol, p-tertiary butyl phenol, p-phenyl phenol, and the like. Such resins are'sold commercially under various trade names, such as Bakelite 254.

The resins may be blended in any desired proportion, although I generally prefer to employ blends containing at least 10%, and more particularly at least 20%, or the lesser constituent. which may be either constituent.

Excellent results are obtained by the use of blends containing from 60% to of a hydrocarbon resin of the type described herein to 20% to 40% of phenolic resin.

Coating compositions of the type described herein usually are prepared by incorporating the resin blend in a drying oil or bodied drying oil, followed by thinning the resulting mixture by the addition of a suitable solvent, such as a hydrocarbon solvent. Driers may be added to the mixture, as well as pigments, coloring agents, plasticizing agents, I antiskinning agents, fillers, and/or other additives.

Examples of drying oils which may .be employed in preparing my new coating compositions are C. for instance from separated ma-' soya bean oil, synthetic and/or modified drying oils and the like.

Examples of thinners are hydrocarbon solvents derived from petroleum oils or cracked products, such as mineral spirits, V. M. 8: P. naphtha, and the like, hydrogenated and/or modified hydrocarbon solvents, coal tar solvents, such as toluol, xylol, and solvent naphtha, and similar materials. Driers which, may be used include the lead, manganese, and/or cobalt salts of high molecular weight organic acids, such as metallic resinates, naphthenates, oleates, and the like.

Pigments which may be incorporated in coating compositions of the type described include white lead, lead chromate, titanium oxide, red lead, zinc oxide, lithopone, chrome yellow, iron oxide, ochre, ultramarine blue, Prussian blue, lampblack, carbon black, and the like.

' A preferred method of incorporating the resin blend in the drying oil comprises heating a mixture of the drying oil and resin blend to a suitable temperature for a period of time sufficient to insure the desired body. The mixture then is reduced to the desired viscosity by the addition of a suitable solvent, such as mineral spirits,

An alternative method comprises heating the drying oil, or a mixture of the drying oil and a portion of the resin blend, to the desired bodying temperature, and adding theresin blend, or the remainder of the resin blend at some stage of the bodying process. After the desired body has been attained, the mixture may be reduced by the addition of a suitable solvent.

The resin blend, or any portion of it, also'may be used to check the bodying of the drying oil at any desired stage.

In addition, the resin blend may be incorporated in a previously bodied or partially bodied oil at a temperature substantially under the bodying temperature of the oil, if desired.

With respect to the oil length of the resulting coating composition, I have discovered that optimum results are secured when oil lengths under 25-gallons, and particularly under 20-gallons, are employed. Excellent results are secured in practically all cases when coating compositions having oil lengths of l-gallons, or less, are employed.

Thus, for example, coating compositions possessing unusually desirable properties are obtained from linseed oil and a resin blend of the type described herein when such compositions have an oil length of from 6 to 10 gallons.

In a similar manner, excellent results have been obtained with both perilla oil and fish oils when the resulting coating compositions have an oil length of -gallons, or less.

At higher oil lengths, the coatingcompositions may be slightly unstable. This is usually manifested by the precipitation of a portion of the resin from the coating composition during storage.

The foregoing preferred oil lengths pertain particularly to coating compositions in which petroleum hydrocarbon fractions such as mineral spirits or V. M. 8: P. naphtha, have been employed as solvents. In case a coal tar solvent, or mixture of coal tar solvent and petroleum hydrocarbon fraction, is used as the solvent, the indicated oil lengths can be increased substantially without seriously impairing the properties of the resulting coating compositions.

The oil lengths discussed in the foregoing paragraphs refer to the number of gallons of drying oil employed for each hundred pounds of resin blend.

The incorporation of a resin blend of the type described herein in a typical 15-gallon varnish is illustrated by the following example.

Example 6 A mixture of parts of the resin prepared as in Example 2 and 20 parts of a phenolic resin derived from the reaction of p-phenyl phenol with formaldehyde is heated with tung oil, in the proportion of 15 gallons of tung oil to pounds of resin, until the'desired body has been attained. The mixture then is cooled and reduced with a mixture of V. M. 8: P. naphtha and xylene to give a varnish containing 50% solids. Upon reaching room temperature, a mixture of lead, cobalt, and manganese naphthenateswas stirred into the varnish.

The varnish possessed outstanding coating properties, giving a quick drying, hard, finish possessing excellent alkali and water resistance on a variety of surfaces.

Coating compositions of this type may be used as such for application to a wide variety of surfaces, or they may be modified by the addition of other ingredients before application.

Thus, for example, pigments may be incorporated in the varnish obtained in Example 6 by blending or mixing in a suitable-mill or other device, such'as a ball -mfll or a roller mill. The incorporation of pigments in such coating compositions is greatly facilitated by the exceptional wetting and dispersing properties of the resin blend of the type described herein, resulting in a marked decrease in the time required to produce a given enamel.

Lesser quantities of other resins may be incorporated in the coating compositions of the type described, if desired. In general, however, I prefer to employ resin. blends of the type described herein as the sole resinous ingredient of the coating composition.

To summarize, the hydrocarbon polymers or resins to which this invention relates may be characterized as follows:

(1) The polymers or resins are comprised of carbon and hydrogen in chemical combination to at least 98% and more particularly, to at least 99%, other elements such as oxygen, nitrogen and/or sulfur derived from the oil pyrolized, if present, being restricted to less than 2%, and more particularly to less than i (2) The polymers or resins are substantially completely soluble in an excess of benzene, the proportion of insoluble material being less than 1%, and more particularly, less than 0.1% of the polymer or resin.

(3) The polymerswr resins have an ash content determined by burning of less than 1%, and more particularly, of less than 0.1%.

(4) Upon subjecting the polymers or resins to destructive distillation under vacuum to effect depolymerization, that portion of the oily material recovered as overhead which boils above 200 C. has a refractivity intercept of at least 1.08 and particularly of at least 1.09 and still more particularly, of at least 1.10.

(5) Polymers or resins hardened by distilling to an overhead temperature between approximately to 200 C. at 20mm. I-Ig absolute pressure in accordance with the procedure of Example 1 have the following characteristics:

(a) They have A. S. T. M. ball and rin softening points of at least 40 C. and more particularly of at least 80 C. For example, typical polymers or resins polymerized by surface active agents such as clay, as catalysts, have A. S. T. M. ball and ring softening points of at least 40 C.. such as between 60 C. and 80 C. or above, and typical polymers or resins polymerized by heat, or with acid or acid-acting catalysts, have A. S. T. M. ball and ring softening points of at least 80 0., such as between 90 and 110 C. and higher, such as up to 120 C. or above.

(b) They have densities of at least 1.10 and up to 1.20 and higher, such as between 1.13 and 1.18, as determined by the water displacement method.

They have molecular weights between 300 and 1000 as determined by the freezing point depression method employing benzene as the solvent. 1 v

(d) They have a solubility in an equal quantity by weight of toluene at a temperature of 20 C. of at least 30 grams, and preferably of at least 50 grams, in 100 grams of toluene.

(e) One part of the polymers or resins when dissolved in three parts by weight of benzene having a density (d 20/4) of 0.8790 and a refractivity intercept of 1.0623, makes fourparts of a solution having a density greater than 0.925 and a refractivity intercept greater than 1.069. Neglecting any possible change that may occur in the solid when it is dissolved, calculated values for the polymers or resins themselves, that is. apart from the solvent, (densities and refractivity intercepts being additive on a volume basis) become for densities at least 1.10, and for refractivity intercepts at least 1.08, and particularly, at least 1.09, and still more particularly, at least 1.10.

(6) The oils from which the polymers or resins are polymerized have mixed aniline points below 15 C., and more particularly, below 10 C., for example, between 10 and 4 C. and lower. A mixed aniline point of a given oil is defined as the critical solution temperature of a mixture of 10 cc. of anhydrous aniline, 5 cc. of the oil being tested and 5 cc. of a petroleum naphtha having an aniline point of 60 C. as determined by A. S. T. M. tentative standard D61l-41T.

(7) The oils from which the polymers or resins are polymerized usually have refractivity intercepts of not less than 1.08, for example, between 1.09 and 1.11, and higher, such as, up to 1.125

(8) The oils from which the polymers or resins are polymerized contain at least 90%, such as not less than 95%, and more particularly not less than 97% of aromatic hydrocarbons.

(9) The oils from which the polymers or resins are polymerized have densities 01' not less than 0.95, and, more particularly, of not less than 0.98, for example, between 0.99 and 1.02, and higher, such as up to 1.11 or 1.12.

(10) Liquid material extracted from the polymers or resins using a large excess of pentane has refractivity intercepts of at least 1.08 and more particularly, of at least 1.09, and still more particularly, of at least 1.10.

(11) The oil separated from the polymers or resins after polymerization usually has a density or not less than 0.95 and, more particularly, of not less than 0.98, for example, between 0.99 and 1.02 and higher. such as up to 1.11 or 1.12. Such oils separated from the polymers or resins after polymerization also usually have refractivity intercepts of not less than 1.08, for example, between 1.09 and 1.11, and higher, such as up to 1.125 or 1.135, and contain at least such as at least and more particularly, at least 97% aromatic hydrocarbons.

(12) Refractivity intercept when referred to herein is determined by the method described in the Science of Petroleum (1938) vol. 2, beginning on page 1175, and publications referred to therein.

In the specification and in the claim the term a phenol-aldehyde resin, unless otherwise qualified, is intended to embrace resins derived by the reaction of phenol, or substituted phenol. the substituent containing one or more hydroxyl and/or allwl groups (such as methyl, ethyl, etc.) and/or aryl (such as phenyl, tolyl, phenyl methyl, etc.) groups, with an aldehyde, such as formaldehyde.

While various procedures and formulas have been particularly described these are of course subject to considerable variation. Therefore, it will be understood that the foregoing specific examples are given by way of illustration, and that changes, omissions, additions, substitutions, and/or modifications might be made within the scope of the claim without departing from the spirit of the invention, which is intended to be limited only as required by the prior art.

I claim:

A composition comprising approximately 20 parts of a phenolic resin derived from the reaction of p-phenyl phenol with formaldehyde, approximately 80 parts of hydrocarbon resin polymer produced by treating with sulphuric acid a hydrocarbon oil which has been physically separated from tar produced in the vapor phase pyrolysis of petroleum oil and which is free from and of greater volatility than the pitch of said tar, said hydrocarbon oil containing, in addition to hydrocarbons boiling between 210 C. and 450 C. which are not polymerizable by the application to said oil of heat alone but which are polymerizable to catalytic resin polymer by treating said oil with sulphuric acid, other hydrocarbons boiling between 210 C. and 450 C. which are polymerizable to catalytic resin polymer by treating said oil with sulphuric acid but which last-mentioned hydrocarbons are also polymerizable to heat resin polymer by the application to said oil of heat alone, said last-mentioned hydrocarbons being present in said hydrocarbon oil in amount greater than approximately 5% of the total hydrocarbon oil boiling between 210 C. and 450 C., and tung oil in the proportion of approximately 15 gallons of tung oil to 100 pounds of resin.

FRANK J. SODAY.

REFERENCES CITED The following references are of record in the file of this patent:

UNITED STATES PATENTS Number Name Date 1.94:5,"119v Apgar Feb. 6, 1984 2,150,614 Thomas Mar. 14, 1939 2,183,234 Butler Dec. 12, 1939 2,387,259 Hall et al. Oct. 23, 1945 2,387,237 Ault Oct. 23, 1945 

